Method of using viscoelastic vesicular fluids to enhance productivity of formations

ABSTRACT

A process for enhancing the productivity of a formation consists of introducing into the formation a viscoelastic fluid which contains at least one surfactant, at least one quaternary amine polyelectrolyte, water, and a non-aqueous solvent. The surfactant forms aggregation structures or vesicles. The fluid, which significantly enhances fluid viscosity and thermal stability, is particularly effective as a diverting fluid to divert an acid treatment package from a high permeability or undamaged portion of a formation to a low permeability or damaged portion of a formation as well as a fracturing fluid. In addition, the fluid is useful for sand control completion.

This application is a continuation of U.S. application Ser. No. 10/846,994 filed May 14, 2004, which is a continuation-in-part application of U.S. application Ser. No. 10/356,210 filed on Jan. 31, 2003.

FIELD OF THE INVENTION

This invention relates to viscoelastic surfactant based fluids which contain a quaternary amine polyelectrolyte and a method of using such fluids to enhance the Productivity of a hydrocarbon-bearing formation. In a preferred embodiment, the invention relates to the use of well treatment viscoelastic fluids, such as diverter fluids in matrix acidizing, fracturing fluids and fluids for sand control completion.

BACKGROUND OF THE INVENTION

Matrix acidizing, the process of injecting a formation stimulation fluid such as acid or other acid-forming materials that may react with minerals in the formation to increase the formation permeability, is a common method used to stimulate and enhance the Production of hydrocarbons from a hydrocarbon producing formation and remove formation damage caused by drilling mud invasion and clay migration.

For most matrix acid treatments, acid is injected into the reservoir below or above fracturing rates and pressures. To obtain the maximum benefits of matrix acidizing, it is often desirable to treat the entire productive interval of the formation with the stimulation fluid. As the stimulation fluid is pumped, it will preferentially enter the interval of least resistance (lowest stress) or highest permeability and will react with the formation material and open additional flow paths. As a result, the high permeability interval or non-damaged zone receives most or all of the stimulation while the desired low permeability or damaged zones do not receive the desired stimulation. In most cases, the low permeability or damaged zone is the portion of the reservoir that will benefit the least from stimulation. Without proper diversion, the acid, by flowing to the higher permeability zone, leaves the low permeability zone untreated.

Acid treatment is further used to remove formation damage. Standard sand control treatments often use high rate water packs. Before or after placement of gravel with a completion fluid, low-density brine or a linear gel, a large acid treatment is typically pumped to remove the near wellbore formation damage or skins encountered in perforation wells. Thus, a clay acid package is often pumped into the formation before the gravel pack to stabilize the residual clay. The results of these treatments are often directly related to the ability of the acid to remove the near-wellbore damage and connect the wellbore to the formation. In addition to determining the most effective combination of acid blends and volumes for each particular reservoir, treatment design and planning is often performed in order to ensure that the acid is placed across the entire interval. Such staging of acid treatment across the entire interval further serves to treat the damaged portion of the sands.

The successful acid placement in matrix treatments of open hole horizontal wells is even more difficult due to the length of the zone treated and potential variation of the formation properties. A successful diversion technique is critical to place the acid to the location where damage exists. For an ideal acid treatment on a long heterogeneous reservoir, one would prefer the majority of the acid to be injected into damaged or low permeability intervals; the minimum amount of acid being spent in the clean or undamaged reservoir. However acid, a nonviscous fluid, enters into the region with the lowest stress contrast which unfortunately is typical of the cleanest interval or the partially depleted sand. In order to re-direct the stimulation fluids from the non-damaged intervals into the damaged intervals, a pressure differential across the high permeability or non-damaged intervals is preferably created. This pressure differential typically forces the stimulation fluid into new portions of the reservoir that otherwise would not receive the stimulation fluid. Until a sufficient pressure differential is built up in this region, the fluid continues to be injected into the high permeability zones of the interval.

In light of such difficulties, operators and service companies typically attempt to stagger the introduction of acid fluid into damaged intervals. Such methodology more effectively treats all of the requisite intervals. In conjunction with the acid staging of the acid volumes, diverter stages are often pumped to temporarily plug the zones that are taking the acid. Rate increases during the treatment to increase injection pressure and cause diversions also are often attempted. Depending on the formation condition, various diverting techniques, such as particulate diverting agents, or viscous acids, have been used both successfully and unsuccessfully in gravel pack and stimulation treatments for numerous years. With many options of chemical diverting or bridging agents available, the type of product used varies from application to application and in some cases may even cause formation damage by the chemical residues. Previous works also established the model and practice to control the pumping rate to achieve the desired diversion.

The overall success or failure of many acid treatments is often judged by the ability to inject or direct the acid into the damaged or lower permeability zone. Without good diversion, the results of the acid treatment often lead to either incomplete damage removal and/or requirements for uneconomical volumes of treatment fluids. A well developed diverting agent, without formation damage after the treatment, is critical to the success of any matrix acid stimulation treatment and successful sand control completion.

Chemical diverting agents attempt to temporarily block the high permeability interval and divert the stimulation fluids into the desired low permeability or damaged intervals. It is desirable for these viscous gels to be stable at the bottomhole temperature and also to be removable from the formation rapidly after the treatment in order to eliminate any potential damage to the high permeability intervals. One chemical diverting fluid is a gelled hydroxyethylcellulose (HEC) pill wherein the viscosity of the pill influences the injection pressure of the interval it enters. As the pill enters the formation, the viscosity of the pill restricts the injection of other fluids into this area. As the injection pressure increases within this portion of the interval, other sections of the interval break down and begin accepting fluid. This technique is severely limited if the temperature of the gelled HEC exceeds 200° F. Above this temperature, the base viscosity and life of the pill is greatly decreased. Another problem seen with gelled HEC is that the blocked zone may be damaged from the polymeric residue left inside the porous media once the acid treatment is completed.

Foams may also be used as a diverting method for acid stimulation. Foams typically are generated through a blend of surfactants and/or a polymer. One of the popular diverting techniques in gravel packing and stimulation is the use of a foamed KCl or NH₄Cl or a gelled HEC pill. When a fluid with high viscosity enters into the high perm zone which restricts the injection of other fluids into the same zone, the injection pressure begins to increase. As the overall injection pressure increases and overcomes the pressure threshold, the relatively low perm sections of the interval begin accepting the injected fluid. This technique is severely limited by temperature due to the instability of most foamed or gelled pills above 200° F. Above this temperature the base viscosity of the pill is greatly decreased and the life of the pill affected.

Another problem associated with foamed or gelled diverters is the lack of effectiveness in extremely high permeability reservoirs (>500 mD). Foamed or gelled HEC pills have little effect in high permeability reservoirs due to the ability of the formation to allow for “leak-off” of such fluids. Properly sized particles such as silica flour, calcium carbonate, or organic resins, with the ability to effectively pass through the gravel or perforations but plate or “bridge off” on the formation face, have been introduced in these environments. Even combinations of HEC diversion agents, nitrogen, and oil-soluble resins have been field tested. The main problems associated with the solid particles may be the improper sizing causing deep invasion problems that may not readily “clean-up” and cause further damage.

The addition of the polymer may also cause formation damage, as described above, while the use of nitrogen gas tanks and other associated pumping equipment are typically required for foam used as acid stimulation diverting agent. This may not be practical in many cases, especially for offshore acid treatments, as the operation is often limited by available deck space on the rig or vessel. In addition, foams typically become unstable above 250° F.

Another type of viscous fluid diverting agent used to assist in formation stimulation is a surfactant or surfactant mixture. One such viscoelastic fluid forms micelles. These wormlike micelles are sensitive to hydrocarbons. By utilizing this sensitivity, the fluid may selectively block water-bearing zones while the hydrocarbon-bearing zone is unaffected. However, this viscoelastic surfactant fluid typically cannot discriminate between zones with various permeabilities as long as the zones are hydrocarbon-bearing. Further, unlike polymer based fluids which rely upon filter cake deposition to control leak-off to the formation, viscoelastic surfactant agents control fluid leak-off into the formation through the structure size of the micelles. Micellar based VES fluids usually have high leak-off rates to the formation due to the small size of the wormlike micelles. Rapid weaving and breaking of these structures also limits the ability of the micellar based viscoelastic system to control fluid leak-off. The temperature limitations for such a system are generally around 200° F. due to the low stability of micellar structure.

With every type of diverting system available currently, clean-up only occurs with the inclusion of some type of outside source. Time, temperature, and interaction with either reservoir fluids or hydrocarbons are required to remove the diverting agent in place. For example, viscoelastic surfactant acid diverters typically require contact with the liquid hydrocarbon during flowback. Without this interaction the same factors that prevent fluids from entering a portion of the reservoir may also inhibit the ability of the reservoir to produce hydrocarbons.

In summary, the success of a stimulation treatment or gravel packed completion is often dependent on the ability of the diverting agent to force the acid treatment into different portions of the reservoir.

A need therefore exists for a method for diverting the stimulation fluid from high permeability zones to desired low permeability zones by a method which avoids the shortcomings of the prior art. This method should preferably use a composition that does not damage the formation, and is easily removed from the formation.

Another common stimulation technique used to enhance production of hydrocarbon from subterranean formations is hydraulic fracturing which is typically employed to stimulate wells wherein recovery efficiency is typically limited by the flow mechanisms associated with a low permeability formation. During hydraulic fracturing, a fracturing fluid, typically a gelled or thickened aqueous solution containing chemical agents as “breakers” and a suspended proppant, is injected into a wellbore under high pressure and is pumped at high rates. Once natural reservoir pressures are exceeded, the fluid induces a fracture in the formation and transports the proppant into the fracture.

The fracture generally continues to grow during pumping and the proppant remains in the fracture in the form of a permeable “pack” that serves to “prop” the fracture open. In this way, the proppant pack forms a highly conductive pathway for hydrocarbons and/or other formation fluids to flow into the wellbore. The fracturing fluid ultimately leaks off into the surrounding formation. The treatment design generally requires the fracturing fluid to reach maximum viscosity as it enters the fracture which affects the fracture length and width.

An important attribute of fracturing fluids is their ability to be recovered from the formation. Typically, the recovery of the fracturing fluid is accomplished by reducing the viscosity of the fluid to a low value such that it flows naturally from the formation under the influence of formation fluids and pressure. This viscosity reduction or conversion is referred to as breaking. Historically, the application of breaking fluids as fracturing fluids at elevated temperatures, i.e., above about 120-130° F., has been a compromise between maintaining proppant transport and achieving the desired fracture conductivity, measured in terms of effective propped fracture length. Conventional oxidative breakers may react rapidly at elevated temperatures, potentially leading to catastrophic loss of proppant transport. Further, encapsulated oxidative breakers often have limited utility at elevated temperatures due to a tendency to release prematurely or have been rendered ineffective through payload self-degradation prior to release.

Fracturing fluids composed of viscoelastic surfactant forming micelles have been reported in U.S. Pat. No. 6,435,277. Such micellar-type viscoelastic fluids have not been utilized widely in fracturing treatments of relatively low permeability formations because, amongst other reasons, materials have not been available that would enable the maintenance of needed viscosity at the elevated temperatures required for hydraulic fracturing operations. Further, such fluids are often subject to temperature and stability limitations and form emulsions which make the fluid recovery and fracture clean-up difficult. This patent further reports the previous limitation of viscoelastic surfactant fracturing fluids to formations containing clays as well as formations which require soluble salts for inhibiting hydration of clay materials.

A need therefore exists for surfactant based fluids having the ability to suspend proppants which are economical and which exhibit superior properties compared to existing products available on the market. In addition, such products need to maintain requisite viscosity at higher temperatures while being thermally stable without causing damage to the formation.

SUMMARY OF THE INVENTION

The viscoelastic vesicular fluid of the invention contains a surfactant, such as an amphoteric surfactant, water, a non-aqueous solvent, a quaternary amine polyelectrolyte and, optionally, an internal breaker package to break the surfactant gel and reduce the fluid viscosity to water. This system does not require contact with formation fluids, brines, or acids for clean up to provide optimum production.

The viscoelastic fluid of the invention does not cause formation damage and preferably comprises densely packed surfactant aggregations, called vesicles. The inclusion of the polyelectrolyte facilitates the formation of the vesicles and reduces the need for high levels of surfactant. Further, the addition of the polyelectrolyte enhances thermal stability of the fluid.

The Theological properties of the fluid of the invention may be adjusted by varying the pH of the fluid, concentration of surfactant, temperature during usage of the fluid and selection of the polyelectrolyte.

The fluid of the present invention is particularly effective as a diverter fluid since it overcomes the disadvantages of the prior art by providing non-damaging methods for diverting acid stimulating fluids to the low permeability or damaged intervals adjacent to the high permeability or non-damaged intervals.

The viscoelastic surfactant fluid of the present invention is further highly effective in the fracturing of subterranean formations, such as formations surrounding oil or gas wells. The fracturing fluid further typically contains an internal breaker package to break the surfactant gel and reduce the fluid viscosity to water. The preferred internal breaker package consists of at least one oxidative breaker and at least one acid forming agent.

In another embodiment of the present invention, a process for stimulating a formation is described. In one embodiment, a process for injecting a diverting fluid into a formation is described. The injection is carried out at a pressure lower than the fracture pressure of the formation.

In yet another embodiment of the invention, an acid stimulation package is injected into the formation, followed by the optional pumping of a spacer fluid. The diverter fluid is then injected into the formation. The pH of the diverting fluid is then reduced. A second acid stimulation package is then injected into the formation. The diverter fluid is injected into the large pore throat portion of the formation as well as the small pore throat portion of the formation. The small pore throat invasion depth of the diverting fluid is less than the large pore throat invasion depth.

In another embodiment of the present invention, the fluid is pumped, for example, into a relatively low permeability formation at a pressure sufficient to fracture the formation, the relatively low permeability formation having a fracture face engaged by the fluid during pumping. Typically, the formation comprises at least one largely hydrocarbon-bearing zone and at least one largely aqueous zone.

The average viscosity maintained by the fluid is more than 100 cp@ 100 s⁻¹ from ambient temperature to about 300° F., when the fluid is used as diverter fluid, and, when the fluid is used as a fracturing fluid, about 350° F., compared to an upper temperature limit of 275° F. of the prior art wormlike micelle surfactant based fracturing fluids.

Another significant advantage of the viscoelastic fluid of the invention is its response to low pH fluid, such as acid. The prior art micellar systems relied upon interaction with hydrocarbons or formation fluids to reduce viscosity. In contrast, the viscosity of the viscoelastic fluids of the invention may be decreased at low pH. By controlling the time that the acid-forming agent reduces the pH, the time required for the fluid to lose viscosity can be controlled. The resulting product is a fluid that can be broken at a desired time.

BRIEF DESCRIPTION OF THE DRAWINGS

In order to more fully understand the drawings referred to in the detailed description of the present invention, a brief description of each drawing is presented, in which:

FIG. 1A is a Transmission Electron Microscopy (TEM) image which illustrates the vesicle structure of the inventive viscoelastic surfactant fluids.

FIG. 1B is an illustration of the vesicular structure of a diverting fluid within the invention.

FIG. 2 demonstrates the leak-off or invasion permeabilities of the inventive viscoelastic surfactant fluids over time.

FIG. 3 shows the pH dependence of the fluid viscosity of the inventive viscoelastic surfactant fluids on temperature and pH.

FIG. 4 shows the effect of temperature on the viscosity of the viscoelastic surfactant fluids of the invention.

FIG. 5 compares the rheological data of the inventive viscoelastic surfactant fluids with varying amount of quaternary amine polyelectrolyte.

FIGS. 6 and 7 show the relationship of pressure and rate of introduction versus time of injection of acid and two diverting fluids for Examples 2 and 3, respectively.

FIG. 8 demonstrates the rheological profile of the viscoelastic surfactant diverter pill made in Example 1.

FIG. 9 shows the dependence of concentration of the nonaqueous solvent on the fluid viscosity of the viscoelastic surfactant fracturing fluids, as discussed in Example 6.

FIG. 10 demonstrates the effect of the gel breaker on the fluid viscosity of the viscoelastic surfactant fracturing fluids of the invention, as illustrated in Example 7.

FIG. 11 demonstrates the effect of a clay stabilizer on the fluid viscosity of the viscoelastic surfactant fracturing fluids of the invention, as taught in Example 8.

DETAILED DESCRIPTION OF PREFERRED EMBODIMENTS

The viscoelastic fluid of the invention comprises:

-   -   (1) at least one surfactant;     -   (2) at least one quaternary amine polyelectrolyte;     -   (3) water, including, but not limited to, sea water or fresh         water, and     -   (4) a non-aqueous solvent.         These components are preferably combined in percentages that are         appropriate for the formation to be stimulated.

Generally, the fluid contains surfactant(s) of about 1 to about 50 weight percent, preferably about 1 to about 40 weight percent, and even more preferably about 2 to about 20 weight percent, based upon the weight of the fluid. The polyelectrolyte is generally present in ranges from about 0.05% to about 3.0% weight percent, preferably about 0. 1% to about 1% weight percent, and more preferably at about 0.1% to about 0.5% weight percent, based upon the weight of the fluid. The non-aqueous solvents are generally present in ranges from about 0.1 to about 25 weight percent, preferably about 0.5 to about 20 weight percent, and more preferably at about 1 to about 15 weight percent, based upon the weight of the fluid. The remainder weight percent is water.

The quaternary amine polyelectrolyte (“polyquats”) is generally soluble in both aqueous and aqueous-alcoholic media. The quaternary amine polyelectrolyte (“polyquats”) is generally soluble in both aqueous and aqueous-alcoholic media and interacts with the surfactant, thereby enlarging the vesicle size and enhancing the thermal stability of the vesicular structure. For conventional vesicle based viscoelastic fluids, a high concentration of surfactant is required in order to create a dense pack vesicle fluid and generate adequate viscosity for practical applications. With the addition of polyquats, a significant reduction of surfactant concentration is achieved, from originally more than 20 percent to current of about 7%.

Polyquats include derivatives of cellulose ethers, such as carboxymethyl cellulose. Further, suitable polyquats include aminoalkyl celluloses, aminocarbamoyl celluloses, hydroxyethylcellulose as well as betainized cellulose aminoamides.

Exemplary of such polyquats include those cellulose ether derivatives represented by the overall structural formula:

wherein:

R_(cell) is the residue of an anhydroglucose repeat unit, particularly from cellulose;

t is 0 or 1;

X is oxygen;

z is from 50 to about 20,000; and

each R₁, R₂ and R₃ is individually represented by the substituent structural formula:

wherein:

A⁻ is an anion;

a is an integer of from 1 to about 3;

m is an integer of from 0 to about 6;

n is an integer greater than or equal to 0, provided that the level of cationic substitution, CS, defined by the average moles of quaternary nitrogen atoms per mole anhydroglucose repeat unit is greater than 0; preferably n is from 1 to about 25, most 3 to 10, more preferably 3;

p is an integer of from 0 to about 6;

q is 0 or 1;

each R₅ and R₇ is individually ethylene, a propylene or a hydroxypropylene;

R₆ is a di- or trivalent, cyclic, branched or straight chain, saturated or unsaturated hydrocarbon having from 2 to about 6 carbon atoms, provided there are at least 2 carbon atoms between the nitrogen atom and any oxygen atom, such as in the ether substituent or polysaccharide residue;

R₈ is hydrogen, hydroxyl, R_(h), alkyl, carboxyl or alkali metal or amine carboxylate, or other terminal group provided that when q is 0 then R₈ is hydrogen or alkyl; R₈ is preferably hydrogen or alkyl;

each R₉, R₁₀ and R₁₁ is individually R_(h), alkyl, aryl, aralkyl, alkaryl, cycloalkyl, alkoxyaryl or alkoxyalkyl, having at least two carbon atoms separating the oxygen atom in the alkoxyaryl or alkoxyalkyl group from the nitrogen atom, or together with R₆ forms a heterocyclic ring. Such nitrogen substituents include lower alkyls having from 1 to about 3 carbon atoms, such as methyl, or ethyl; aryls such as phenyl; aralkyls such as benzyl; or, together with R₆, dialkyl substituted cycloalkyl such as N,N-dimethyl pyrrolidyl; and the like. Preferred nitrogen substituents of each repeat unit are methyl, a hydrophobic group, or together with R₆ provides a pyrrolidyl, or are a mixture of such groups;

R_(h) is a hydrophobic group containing an alkyl group having at least 8 carbon atoms, preferably from about 10 to about 24 carbon atoms, and most preferably from about 10 to about 18 carbon atoms;

v is equal to the valence of A, preferably 1; and

y is 0 or 1, provided that when y is 0 then p and q are 0 and R₈ is hydrogen or other terminal group.

In a preferred embodiment, z is from about 100 to about 6,000; and most preferably from about 250 to about 4,000. The corresponding molecular weights of the cationic cellulose ether ranges typically from several thousand up to several million.

Exemplary anions for A⁻ include inorganic anions such as chloride, bromide, iodide, sulfate, methylsulfate, sulfonate, nitrate, phosphate and the like; and organic anions such as acetate and the like. Monovalent anions are preferred, particularly halides and especially chloride. The anions are typically provided as the residue of the quaternary ammonium salts used as quatemizing agents, or by other known techniques.

The number of quaternary nitrogen atoms per substituent, defined by n in Formula III, is greater than or equal to 0. The extent of quaternization throughout the polysaccharide, characterized as the degree of cationic substitution, i.e., CS, provides an average value per repeat unit which is greater than 0, and in some embodiments is generally less than 1 and preferably from about 0.01 to about 0.6.

Such cellulose ether derivatives of formula (I) are disclosed in U.S. Pat. No. 4,767,463, herein incorporated by reference. In a particularly preferred embodiment, the cellulose ether is polyquatemium-4 represented by the structural formula:

Polyquaternium-4 or quaternized hydroxyethyl cellulose is manufactured by National Starch and Chemical Corporation under the trademark Celquat. The viscous grade H-100 is especially effective. It is supplied as a granular powder which is soluble in water.

Further preferred polyquats include those of the general formula:

wherein

b is between 2 and 8, preferably 4 or 5; and wherein:

R¹ is hydrogen or methyl, preferably hydrogen;

R² is a divalent aliphatic hydrocarbon group with 2 to 20 carbon atoms, preferably —CH₂—CH₂— or —CH₂—CH₂—CH₂—;

R³, R⁴, R⁶, R⁷ and R⁸ are alkyl groups with 1 to 4 carbon atoms that may be the same as one another or different from one another, and are preferably each methyl groups;

R⁵ is a substituted or unsubstituted divalent aliphatic group with 2 to 5 carbon atoms, preferably —CH₂—CH(OH) —CH₂—; and

X¹ and X² are anions that may be the same as one another or different from one another; preferably a halide, a sulfate ester group, or a sulfonic acid group, most preferably chloride.

Such polyquats are disclosed in U.S. Pat. No. 6,071,505, herein incorporated by reference, and typically may have at least about 0.2 polyquaternary ammonium groups present for each anhydroglucose unit of the polymeric molecule, preferably between about 0.3 and about 0.7 diquaternary groups per anhydroglucose unit, most preferably about 0.5.

Further exemplary polyquats include ammonium derivatives of cellulose ethers, aminoalkyl cellulosics, aminocarbamoyl cellulosic material, hydroxyalkylcellulose as well as betainized cellulose aminoamides.

Viscoelastic fluids not containing polyquats typically lose viscosity upon dilution with water or mixing with hydrocarbons. The effect of temperature on viscosity in the viscoelastic surfactant fluids of the invention versus those fluids containing no polyquat is illustrated in FIG. 4.

The water may be fresh water or salt water. The water may also contain a salt. Useful salts include, but are not limited to, potassium chloride, sodium chloride, cesium chloride, ammonium chloride, calcium chloride, magnesium chloride, sodium bromide, potassium bromide, cesium bromide, calcium bromide, zinc bromide, sodium formate, potassium formate, cesium formate, sodium acetate, and mixtures thereof. The percentage of salt in the water preferably ranges from about 0% to about 60% by weight, based upon the weight of the water.

The viscoelastic fluid of the invention is characterized by its vesicle structure. FIG. 1A is a Transmission Electron Microscopy (TEM) image which illustrates the vesicle structure. Such vesicles are best described as a “water-in-water” emulsion. A schematic drawing of the vesicle 15 is illustrated in FIG. 1B. Vesicle core water 10 lies at the approximate center of the vesicle structure. The surfactant chains 20 have a hydrophilic end 23 and hydrophobic end 24. The surfactant chains 20, composed from at least two surfactant molecules, 21 and 22, are formed from the attraction of hydrophobic ends 24 of the surfactant molecules. At least one hydrophilic end 23 of surfactant chain joins vesicle core water 10. Water 30 surrounds vesicle 15. Among the surfactant chain 20 is non-aqueous solvent 40 that facilitates the structure of the vesicle. The representative vesicle shown in FIG. 1B is unilamellar. A multilamellar vesicle structure is similar in structure, with surrounding water 30 becoming a new core water layer for the next layer of surfactant chains.

The vesicles are classified by the structure of surfactant aggregations in water. Such vesicles provide adequate viscosity for acid diverting purpose and may be characterized as bi-layered aggregates. The diameter of the vesicle generally varies from between about 100 Å to about 50 microns. The size of the aggregation structure of the vesicles is typically much larger than the wormlike micelles. This increase in aggregate structure size creates a much larger surface area. Typically, the vesicle is circular like a ball, in contrast to the wormlike rod-shaped micelles of the prior art. The diameter of the vesicle ball of the invention generally is about the same as the length of the rod-shaped micelles of the prior art. The vesicle structure is also a more stable system than the micellar system and does not continually lose shape and reform over time like the wormlike micelles. Vesicles in a particular system are not necessarily of a uniform size and may have a wide distribution. When the term “vesicle” is used herein it is meant to mean both unilamellar and multilamellar vesicles.

The fluid viscosity for the diverting fluids of the invention may principally be attributed to the vesicular structures aggregated through interaction of surfactant molecules. The surfactant molecules form vesicles through physical interactions and once the physical condition changes, the vesicle structure changes and fluid loses its viscosity.

Many different types of surfactants may be used to form the viscoelastic surfactant fluids. For instance, the mixture of a cationic and an ionic surfactant with water and a non-aqueous solvent will form such a vesicle. Double-tailed surfactants, amphoteric surfactants, and anionic surfactants may also be used. The typical surfactant molecules for this type of fluid are molecules with molecular weight around several hundreds. The surfactant may be chemically or enzymatically modified.

Examples of suitable surfactants forming the aggregated vesicles include, but are not limited to, imadazoline, alkyl betaine, alkyl amine oxide, phospholipids and lecithin. In a preferred embodiment, the lecithin may be obtained from soybeans. The lecithin may be natural or synthetic lecithin. Preferred phospholipids and lecithin include phosphatidylcholine, phosphatidylethanolamine, and phosphatidylinositol. Additional information on lecithin and its many variants, may be found in Kirk-Othmer Encyclopedia of Chemical Technology, 4^(th) ed. Volume 15, pages 192-210, John Wiley & Sons, 1995, Lecithins Sources, Manufacture & Uses, by Bernard F. Szuhaj, American Oil Chemists' Society, 1985 and Lecithins, by Bernard F. Szuhaj and Gary R. List, American Oil Chemists' Society, 1985.

The introduction of polyquat as electrolyte further reduces the minimum amount of surfactant required for vesicle formation. Before the addition of the electrolyte, almost 27% by volume surfactant loading is minimally required in order to generate adequate viscosity for oilfield applications. Upon the addition of electrolyte to 10 weight percent surfactant, gelation commences and the final viscosity of the vesicular fluid is dependent upon the loading of the quaternary amine electrolyte. This phenomena is further evident by observation of the vesicular fluid in FIG. 1. To generate the fluid viscosity seen in a vesicular fluid containing no polyquat, more surfactant is required as the number and size of vesicles in the fluid increase. The reduction in surfactant concentration further makes it possible to minimize the potential of emulsion formation. In fact, no emulsion has been observed in either laboratory or field usages of the inventive vesicular fluids.

When used as a fracturing fluid, the polyquat further is useful to reduce clay swelling attributable to clay stabilizers.

The viscoelastic surfactant fluids of the invention are further sensitive to pH. As illustrated in FIG. 3, the inventive diverting fluids may lose structure and viscosity at low pH. This is particularly beneficial in applications of acid diverting since it ensures complete gel breaking during the acid pumping stage, leaving no damage to the high permeability zone. The pH of the fluid should preferably be above 9.0, preferably between about 9.0 and about 11.0.

The non-aqueous solvent is typically one or more hydrocarbons and/or halogenated hydrocarbons, although other non-aqueous solvents also function appropriately. Examples of the non-aqueous solvents include, but are not limited to, aliphatic hydrocarbons, aromatic hydrocarbon, alcohols, mineral oils, organic oils such as a soybean oil or a corn oil, fatty acids, glycol ethers, ethers, or mixtures thereof. An example of an alcohol useful in the composition is a linear, branched, or cyclic C₁ to C₂₀ alcohol, such as a linear or branched C₄ to C₂₀ alcohol. Examples of these solvents are 2-ethyl hexanol, ethylene glycol monobutyl ether, ethylene glycol monobutyl, or mixtures thereof.

When employed as a diverter fluid, the inventive viscoelastic fluids of the invention may optionally include an internal breaker to ensure complete breaking at desired time intervals. When used as a hydraulic fracturing fluid, the inventive viscoelastic composition of the invention typically include an internal breaker. Use of the internal breaker ensures that the viscous gel will be broken without leaving residual damage to the higher permeability formation. Without the internal breaker, the time required for the fluid to lose viscosity is most easily controlled by monitoring the effect of the acid-forming agent on the pH of the fluid. Generally, after the diverting fluid is broken, the formation will return to the same permeability as before the diverting fluid was applied.

Suitable internal breakers for use in the invention may be an ester, an organic or inorganic acid, an anhydride, an acid halide, a polyglycolic acid or mixtures thereof. Examples of these include, but are not limited to, methyl formate, ethyl formate, propyl formate, butyl formate, methyl acetate, ethyl acetate, propyl acetate, butyl acetate, ethylene glycol monobutyl acetate, ethylene glycol diacetate, acetic anhydride, acetic formic anhydride, succinic anhydride, tetrachlorophthalic anhydride, chloro ethyl formate, chloro ethyl acetate, polyglycolic acid, ethylene glycol diacetate, ethylene glycol triacetate, and the like and mixtures thereof. The internal breaker may also be an oxidizer such as, but not limited to, persulfates, such as ammonia persulfate and sodium persulfate, and peroxidizers such as hydrogen peroxide. These compounds may also be used in combination when desired.

When used as a fracturing fluid, the inventive viscoelastic composition of the invention typically include an internal breaker to ensure complete breaking at the desired time intervals. Typically, the internal breaker used with the fracturing fluid is a combination of at least one oxidative breaker and at least one acid forming agent. The percentage of internal breaker in the fluid is typically dependent upon the type of internal breaker and the desired time for reducing the fluid pH. By controlling the time in which the acid-forming agent reduces the pH, the time required for the fluid to lose viscosity may be controlled, creating a fluid that can be broken at a desired time.

The percentage of internal breaker in the fluid will typically depend upon the type of internal breaker and the desired time for reducing the fluid pH. The internal breaker may range from about 0.001 to about 10% of the total fluid, preferably 0.001-5%, most preferably 0.003-2%, all by weight, but may be higher or lower if desired. When used in fracturing fluids, the weight percentage of the two breakers in the internal breaker system is typically between from about 0.001% to about 1% oxidative internal breaker and the remainder being the acid forming agent. The combination of acid, temperature and internal breaker ensures that the fluids of the invention will be broken during or after treatment. Such properties have particular applicability in both dry gas and oil bearing reservoirs.

The oxidative internal breaker is preferably, but not limited to, persulfates, such as ammonium persulfate, sodium persulfate, encapsulated ammonium persulfate, potassium persulfate, encapsulated potassium persulfate, and peroxidizers such as inorganic peroxides (including encapsulated inorganic peroxides) like hydrogen peroxide, organic peroxides (including encapsulated organic peroxides) as well as sodium perborate (including encapsulated sodium perborate), as well as sodium bromate, sodium perforate, potassium iodate, potassium periodate, sodium chlorite, sodium hypochlorite, lithium hypochlorite and calcium hypochlorite or a mixture thereof.

The acid forming agent, preferably acting as a companion to the oxidative breaker, is any substance which is initially inert but slowly hydrolyzes in the fracturing fluid to produce a Bronsted acid, thereby gradually lowering the pH of the fluid and activating the oxidative breaker. The preferred acid forming agent includes organic anhydrides, acyl halides, sulfonyl halides, benzylic halides and low molecular weight esters which slowly hydrolyze to produce Bronsted acids. By “low molecular weight” ester is meant that the ester should be soluble in the fracturing fluid in order to accomplish its intended purpose of hydrolyzing with time to produce an acid. Generally, the higher the molecular weight, the less soluble the ester. As a result, lower molecular weight esters are preferred for ease of use. Preferably, the acid forming agent is a low molecular weight ester selected from the group consisting of ethyl acetate, 2-ethoxyethylacetate, ethylacetoacetate, triethylcitrate, methylbenzoate and dimethylphthalate.

The stimulation fluid of the invention may further other components conventionally used in the art. For instance, the fluid may include a demulsifier or non-emulsifier, fluid loss additive, mutual solvent, etc. Where the stimulation fluid is a diverter fluid, an acid or corrosion inhibitor may further be employed. Acids may include inorganic acids such as hydrofluoric, hydrobromic, hydrochloric, and H₂CO₃, and organic acids such as acetic acid, formic acid, and citric acid. Mutual solvents include such compounds as ethylene glycol monobutyl ether, and dipropylene glycol methyl ether. The diverter fluid may be used with a spacer fluid such as a salt solution of NaCl, KCl and/or NH₄Cl. Such components are present in an amount between from about 0.05% to about 10%, preferably from about 0.05% to about 5%, weight percent of the total weight of the fluid.

In addition, the fluid of the invention may contain a gas such as carbon dioxide or nitrogen, and the like. This fluid preferably contains less than 30% gas by volume, preferably less than 10%, and most preferably less than 5% gas.

Invasion or the leak-off profile of the viscoelastic fluid of the invention may be controlled by the size of the surfactant aggregated structure. With the viscoelastic fluids of the invention, the size of the aggregation structure of the system is large. The physical size of the vesicles of the invention are much larger than the prior art wormlike micelles. In particular, the generally ball-shaped vesicles are three-dimensional in contrast to the one-dimensional rod-like micelles of the prior art. The ball-shaped vesicles of the invention are stable and do not continually lose shape and reform over time. Thus, the vesicles formed by the surfactant aggregates render a viscoelastic system having greater ability to control fluid leak-off and invasion. In particular, an operator may control leak-off of the stimulating fluid to the formation by controlling the size differential between the vesicles and the pore throats. As the size differential increases, for example, because of a permeability decrease or damage, the invasion of the vesicles into the formation is reduced. Conversely as the size differential decreases, for example, because of a permeability increase, the invasion into the formation increases.

As such, the VES fluids of the invention do not generally form filter cake and behave similarly in leak-off tests as other VES fluids. Further, in most cases, they exhibit less leak-off than the wormlike VES micellar type fluids of the prior art in middle permeability formations.

Further, the thermal stability of the vesicular structure of the fluid is greatly improved over the conventional surfactant vesicle structures or the wormlike micelles of the prior art.

Without its use as a diverting fluid, the stimulating fluid would normally be injected into the portion of formation at the point of least resistance during matrix injection. This portion of the formation is typically associated with the highest permeability or least amount of formation damage. An injection pressure increase in the high permeability or undamaged portion of the formation or diverting agent would be required to change the injection profile. When used as a diverter fluid, once the viscous fluid is in place in the formation, it will have a finite depth of invasion related to the pore throat diameter. Typically, for a given formation type, the invasion depth is directly proportional to the nominal pore throat diameter of the formation. As the fluid stops moving in the formation, the amount of injection pressure into this interval will also increase. At some point during injection, the pressure required to inject the stimulation fluid into this interval will exceed the pressure required to inject the stimulation fluid into other portions of the interval and diversion will be achieved.

The viscous pill may be placed across the entire formation. Varying depths of invasion will then occur throughout the formation based upon the varying permeability or damage throughout the interval. The ability of the viscoelastic fluid to invade into these pore throats will vary depending on the difference between pore throat sizing of the damaged and non-damaged formation materials. Invasion depths will normally be greater in the cleaner or non-damaged portion of the formation (larger pore throats) than in the lower permeability or damaged zones (smaller or partially filled pore throats). With a greater depth of invasion in the cleaner sections of the formation, more of the diverting pill may be placed in these intervals.

FIG. 2 demonstrates the leak-off rate of a viscoelastic fluid of the invention in a formation with differing permeabilities, specifically in a 2 inch core at 180° F. with permeabilities of 50 mD and 500 mD wherein the leak-off volume is represented by the y-axis and where mD is the unit for permeability. The fluid has a much higher leak-off in the high perm core (500 mD) (deeper invasion into the formation) than that in a low perm core (50 mD). The returned penn on the core flow tests were accessed by flowing the core with 3% KCl to obtain the permeability of the core, pushing the diverting fluid (as a pill) through the core to create the plug, flowing the core again with 3% KCl to obtain the returned permeability of the core, the “returned perm.” If the second reading on the permeability is the same as the original value, the returned permeability is 100%. The results indicated 90% returned perm without breaker and 100% returned perm with the addition of internal breakers.

Thus, when the fluid of the invention is pushed into a production zone, as diverting fluid, with various permeabilities, the majority of the diverting fluid will enter into the high permeability or non-damaged zone and form a temporary plug or viscous pill while the lower permeability zone has little invasion. This temporary viscous pill causes a pressure increase and diverts the fluid to a lower permeability portion of the formation.

Conventionally, the pill is pumped behind the stimulation fluid and enters the same portion of the formation as the stimulation fluid. A temporary “bridge” is formed. The viscoelastic pill has varying depths of invasion based upon permeability or damage to the interval since the plug and the pill enter across the entire formation. The annulus pressure increases and the acid stage, following introduction of the diverter, directs the acid to other portions of the interval. The diverting fluid of invention may also have an internal breaker built into the system to insure that the fluid viscosity can be reduced after a period of time.

Throughout the treatment, as injection is continued and pressure decreases, due to the removal of damage in other portions of the interval or the loss of viscosity of the diverting pill, additional diverter stages may be pumped. By alternating the pumping of acid stimulation fluids and diverting fluids, the heterogeneous formation may be appropriately treated. A typical pumping schedule may be as follows:

-   -   (1) Injecting an acid stimulation fluid package;     -   (2) Optionally pumping a spacer fluid;     -   (3) Injecting a viscoelastic surfactant diverting fluid;     -   (4) Optionally, followed by pumping a spacer fluid; and     -   (5) Repeat step 1 to 4 as necessary.         Preferably, the injection pressure of the diverting fluid is         less than the fracture pressure of the formation. This fracture         pressure will depend upon the type of formation.

The final injection pressure of the spacer fluid or acid stimulation fluid will generally be lower than original injection pressure, demonstrating damage removal or stimulation of portions of the zone that were not included in the initial injection. If necessary, steps 1 to 4 may be repeated to improve the placement of stimulation fluids by monitoring the treating pressure, bottom hole pressure, or surface pressure reading.

A reduction in pH of the vesicle structured viscoelastic fluid will cause a reduction in the fluid viscosity. In most stimulations, a stage of acid is injected following the diverting stage. As the stimulation fluid enters the formation and comes in contact with the viscous pill, the acid or low pH fluid will reduce the pill's viscosity. As the viscosity of the pill is reduced, fluid enters that portion of the reservoir. Because the diverting fluid will most often have less penetration into the damaged or less permeable section of the formation, there is less diverting fluid in the damaged or less permeable section of the formation in a bulk sense. As a result, acid from a later acid treatment or resulting from the acid-forming compounds of an internal breaker will remove all or nearly all of the diverting agent from the damaged or less permeable section of the formation before that of the undamaged or more permeable section. This action allows penetration of the acid treatment in the damaged or less permeable section of the formation before that of the undamaged or more permeable section. The oxidizing agent type of internal breaker is believed to result in the same effect, but by a different mechanism of actually breaking up the surfactant chains of the vesicles. With less of the pill volume in the lower permeability zones, viscosity loss normally occurs more rapidly. As the viscosity of the pill is reduced, and with less volume in the damaged interval, the pressure restriction causing diversion is normally reduced and the stimulation fluid enters that area of the formation. This formation invasion profile is a reason for the successful diversion of the acid treatment.

The viscoelastic fluid of the invention more readily loses its viscosity (and thus structure) at lower pH, as shown in FIG. 3. FIG. 3 is a graphical depiction illustrating the dependence of the viscosity of the fluid of the invention on temperature and pH. Diverting fluid line 400 depicts the viscosity of the diverting fluid of one embodiment of the invention at a pH of 12.0, fluid line 500 at a pH of 1 1.0, fluid line 600 at a pH of 10.0 and fluid line 700 at a pH of 9.0. The pH of the fluid may be adjusted when desired. Typically, the pH is maintained at a value of between about 9.0 to about 11.0. The pH may be adjusted by any means known in the art, including the addition of acid or base to the fluid, or bubbling CO₂ through the fluid and the like.

The fluids of the invention are easy to use and can be prepared on site or off-site. When used as a fracturing fluid, the inventive fluids exhibit excellent proppant carrying capacity including any proppant used with the viscoelastic fluids of the prior art.

EXAMPLES

The following examples will illustrate the practice of the present invention in preferred embodiments. Other embodiments within the scope of the claims herein will be apparent to one skilled in the art from consideration of the specification and practice of the invention as disclosed herein. It is intended that the specification, together with the example, be considered exemplary only, with the scope and spirit of the invention being indicated by the claims which follow.

Viscosity measurements were conducted on a Fann 50C viscometer while the respective sample was sheared at 100 s⁻¹ constantly while the temperature was raised to the stated test temperature. The pressure readings were recorded through field applications of the fluid. Examples 2 and 3 are studies resulting from the injection into an oil well in the Gulf of Mexico having a bottomhole temperature ranging between 150 and 200° F.

Example 1

About 0.3 g of a carboxymethyl cellulose containing a quaternary amine group, commercially available as CELQUAT® H-100 polyelectrolyte (from National Starch & Chemical) was added to 90 ml of water, as an aqueous solvent, in a Waring blender. The mixture was agitated for approximately 30 minutes. About 2.4 ml of ethylene glycol monobutyl ether was added under agitation, followed by 7.6 ml of lecithin (Riceland Chemical). Agitation was continued for another 10 minutes. The pH of the solution was then adjusted to 10.0 using a 30% NaOH solution and the solution was agitated for another 10 minutes. The fluid was poured out and a viscosity test was then run on a Fann 50. The results of the rheological measurements are set forth in FIG. 8. FIG. 8 further illustrates the effect of temperature on viscosity of the viscoelastic surfactant fluid of the invention.

Example 2

A viscoelastic surfactant diverter pill, made from the preparation in Example 1, was used in a 53-foot oil-bearing reservoir at a measured depth of 14,500 feet. Bottomhole temperature in this interval was recorded at 198° F. and the interval was completed as a high rate water pack (HRWP). A 10% HCl −5% acetic acid treatment was injected in stages in front of the gravel to remove the damage and improve connection to the near-wellbore region. The acid treatment was separated into three stages to best treat the entire interval with two diverter pills.

After injecting the first HCl/acetic acid into the formation, the treating pressure on the annulus decreased from 1,300 psi to less than 250 psi at a rate of 1.5 bpm (See FIG. 6). The annulus pressure stabilized during treatment of the well with a 5% NH₄Cl spacer fluid. The viscoelastic diverter pill was injected into the well. Once the viscoelastic diverter pill reached the perforations, an increase of 1200 psi in annulus pressure was observed as the rate was held constant at 3 bpm. Most of this pressure increase can be associated with the diverter pill since the pumping rate was kept fairly stable.

Following the placement of the first diverter pill, a second stage of HCl/acetic acid treatment was injected into the formation at 3 bpm. Once the acetic acid/HCl entered the formation, the pressure decreased from 1300 psi to 400 psi on the annulus. The pressure response is indicative that the fluid entered the portion of the damaged or lower perm interval and clean-up of this portion of the perforated interval occurred.

As the second diverter pill was introduced into the formation, the annulus pressure increased from previous 400 psi up to 1400 psi over several minutes while the pumping rate was kept at 3.5 bpm. This pressure increase can be attributed to the viscosity effect of the viscoelastic diverter pill inside the porous formation. Following the introduction of the second diverter, the last stage of HCl/acetic acid was injected. Once this portion of the acid was on the formation, the annulus pressure dropped in several minutes. Although part of the acid enters the temporarily bridged zone, a good portion of the acid would be diverted into some portion of the reservoir unstimulated by the previous two stages of acid. This could be indicative of acid diversion and clean-up in a new portion of the perforated interval or indicative that the diverter pill had lost viscosity and the effective “bridging” or diversion.

The HRWP was pumped as designed with an annular screen-out occurring and the well was producing above expected production rates.

The pressure responses demonstrate that there is no injection restriction after the introduction of the diverter fluid followed by acid stimulation. Further, it indicates that no damage is caused by the diverter fluid. Additional pills can be added to the treatment to promote additional diversion, if necessary. No emulsion was formed in this Example.

Example 3

In this Example, the viscoelastic diverter pill of Example 1 was used in a 120 ft gross and 91 ft net oil reservoir at a measured depth of 9,600 feet. The well was not perfectly deviated by 41 degrees. The primary in a single selective, this zone was completed as a HRWP. The bottomhole temperature in this interval was recorded at 150° F. A 10% HCl acid solution was injected in front of the gravel to improve connection to the near-wellbore region. The acid treatment was separated into four stages with three viscoelastic diverter pills.

Once the first acetic-HCl acid stage reached formation, the treating pressure on the annulus decreased from 450 psi to 200 psi (See FIG. 7). As injection was continued with the HCl acid and the acid rate was increased from about 2 bpm to about 3.0 bpm, the annulus pressure continued to decrease. The (first) viscoelastic diverter pill was injected at the rate of 3.0 bpm and once the diverter pill reached the perforations, a 300 psi increase in annulus pressure was observed at a rate of about 3.0 bpm. Following the placement of the first diverter pill, the second stage of treatment acid was injected into the formation at 3.0 bpm. A stabilized pressure injection profile was observed over the next 5 minutes as the second stage of 5% NH₄Cl spacer and HCl acids were injected into the formation. As the second stage of HCl entered the formation, the pressure decreased from 500 psi to about 300 psi on the annulus. The injection rate of the acid was increased to 3.75 bpm and the (second) diverter pill was injected.

Once the diverter reached formation, a 300 psi pressure increase was observed in the annulus. Following the second diverter, the third stage of HCl was injected at the rate of 6 bpm. There was a 5 minute period in which the annulus pressure stabilized at about 650 psi and then rapidly decreased to about 500 psi once the acid entered into the non-treated zone and breakdown of the formation occurred. (This could be indicative of acid diversion and clean-up in a new portion of the perforated interval or that the diverter pill had lost viscosity and the effective “bridging” or diversion.)

A third diverter pill was pumped and followed by the last stage of the acid treatment. A 200 psi pressure increase was observed in this stage of the diverter. Once the last stage of the acid entered the formation, 5% KCl was pumped to flush the formation and the step rate test was started. The HRWP was pumped as designed with an annular screen-out occurring and the well was producing above operator expectations.

The pressure responses demonstrate that there is no injection restriction after the introduction of the diverter fluid followed by acid stimulation. Further, it indicates that no damage is caused by the diverter fluid. Additional pills can be added to the treatment to promote additional diversion, if desired. No emulsion was formed in this Example.

Example 4

This Example illustrates that the viscoelastic surfactant fluids of the invention are sensitive to pH and demonstrates the effect of pH on viscosity of the viscoelastic surfactant fracturing fluid of the invention.

Four base fluids were made as following: 0.3 g of CELQUAT® H-100 polyelectrolyte was added to 90 ml of water, as an aqueous solvent, under continuous agitation for 30 minutes, followed by 1.2 ml of ethylene glycol monobutyl ether and then 8.8 ml of lecithin while under agitation.

Fluid #1: the pH was adjusted to 9.0 using a 30% NaOH solution and agitation was continued for another 10 minutes.

Fluid #2: the pH was adjusted to 10.0 using a 30% NaOH solution and agitation was continued for another 10 minutes.

Fluid #3: the pH was adjusted to 11.0 using a 30% NaOH solution and agitation was continued for another 10 minutes.

Fluid #4: the pH was adjusted to 12.0 using a 30% NaOH solution and agitation was continued for another 10 minutes.

The viscoelastic surfactant fracturing fluid used the invention more readily loses its viscosity (and thus structure) at lower pH, as shown in FIG. 3. This is particularly beneficial since it ensures complete gel breaking during the pumping stage, leaving no damage to the high permeability zone. The pH of the fluid may be adjusted when desired. Typically, the pH is maintained at a value preferably above 9.0, typically between about 9.0 to about 11.0. The pH may be adjusted by any means known in the art, including the addition of acid or base to the fluid, or bubbling CO₂ through the fluid and the like. FIG. 3 is a graphical depiction illustrating the dependence of the viscosity of the viscoelastic surfactant fracturing fluid on temperature and pH.

Example 5

This Example illustrates the effect of polyquat polyelectrolyte loading on viscosity of the viscoelastic surfactant fracturing fluid of the invention.

Three base fluids were made by adding:

Fluid #1:0.2 g of CELQUAT® H-100;

Fluid #2:0.3 g of CELQUAT® H-100; and

Fluid #3:0.4 g of CELQUAT® H-100 to 90 ml of water, as an aqueous solvent, under continuous agitation for 30 minutes, followed by 1.2 ml of ethylene glycol monobutyl ether and then 8.8 ml of lecithin while under agitation. The pH of each fluid was adjusted to 10.0 using a 30% NaOH solution and agitation was continued for another 10 minutes.

The viscosity of each fluid was then measured while the temperature was raised to each test temperature. FIGS. 4 and 5 compare the rheological data between viscoelastic fluids with varying amounts of polyquat. Specifically it demonstrates the change in viscosity at elevated temperatures of fluids containing 0.2 weight percent polyquat, 0.3 weight percent polyquat and no polyquat but an increased level of surfactant. A vesicle fluid having no polyquat exhibits the thermal stability at about 250° F. With the introduction of polyquat, it is possible to stabilize the viscoelastic fluid up to about 350° F. The positively charged polyquat has strong interaction with the surfactant molecules which thereby result in more stable vesicles. Compared to the vesicular fluid containing no polyquat, the vesicular structure of the invention containing a polyquat is larger and more diverse in size. This character is likely attributed to the interaction of the polyquat with surfactant molecules. This strong interaction makes it possible to have more and larger vesicles than the vesicle fluids containing surfactant only. As shown in FIG. 1, the vesicle structures of the invention have concentric rings and are typical of multilayered surfactant vesicles.

Thus, the rheology of inventive vesicle fluid further depends on the loading of polyquat. As shown in FIG. 4, the vesicular fluid with polyquat as electrolyte has lower viscosity at lower temperatures than the vesicular fluid void of polyquat and having higher surfactant loading. When the loading of the polyquat reaches 0.3%, the fluid has similar viscosity at lower temperatures to that of the fluid without polyquat. At higher temperatures, the vesicular fluid with polyquat has significantly higher viscosity than the vesicular fluid void of polyquat. Thus, the vesicular fluid increases its viscosity as the loading of polyquat increases; however, the increment in loading of polyquat does not further enhance vesicular structure and viscosity. Because of the reduced surfactant loading, the potential of emulsion formation between the fracturing fluid and the produced hydrocarbon is reduced.

Example 6

This Example illustrates the effect of nonaqueous solvent loading on viscosity of the viscoelastic surfactant fracturing fluid of the invention.

Four base fluids were made as following: 0.3 g of CELQUAT® H-100 was added to 90 ml of water, as an aqueous solvent, under continuous agitation for 30 minutes, followed by:

Fluid #1:1.2 ml of ethylene glycol monobutyl ether and then 8.8 ml of lecithin while under agitation;

Fluid #2:1.9 ml of ethylene glycol monobutyl ether and then 8.1 ml of lecithin while under agitation;.

Fluid #3:2.4 ml of ethylene glycol monobutyl ether and then 7.6 ml of lecithin while under agitation; and

Fluid #4:2.9 ml of ethylene glycol monobutyl ether and then 7.1 ml of lecithin while under agitation.

The pH of each fluid was then adjusted to 10.0 using a 30% NaOH solution and agitation was continued for another 10 minutes.

The viscosity of each fluid was measured while the temperature was raised to the test temperature. The viscosity was measured and the results of the rheological measurements are set forth in FIG. 9. FIG. 9 demonstrates that a window of solvent concentrations is suitable. For instance, as shown by Fluid #1 and Fluid #2, a peak at higher concentrations at certain temperatures is evidenced.

Example 7

This Example illustrates the effect of a gel breaker on viscosity of the viscoelastic surfactant fracturing fluid of the invention.

0.3 g of CELQUAT® H-100 was added to 90 ml of water, as an aqueous solvent, under continuous agitation for 30 minutes, followed by 1.9 ml of ethylene glycol monobutyl ether and then 8.1 ml of lecithin. The pH of the solution was adjusted to 10.0 using a 30% NaOH solution and agitation was continued for another 10 minutes.

A breaker package, containing 1 ml of triethylcitrate and 0.042 g ammonium persulfate was added to the fluid immediately before the fluid was placed on the Fann 50C viscometer and sheared at 100 s⁻¹ constantly while the temperature was raised to the test temperature, 140° F. Viscosity of the fluid was measured under 100 s−1 constant shear during the course of the test while the temperature was maintained at 140° F. The fluid viscosity started dropping to below 100 cp after about 210 minutes. The results of the rheological measurements of the fluid are shown in FIG. 10.

The combination of temperature and internal breaker ensures that the fracturing fluids of the invention will be broken during or after treatment. The optional internal breaker therefore assists to ensure that, even without acid interaction, the viscous gel will be broken and will not leave residual damage to the higher permeability formation. Generally, after the fracturing fluid is broken, the formation will return to the same viscosity as before the fracturing fluid was applied.

Example 8

This Example illustrates the effect of a clay stabilizer on viscosity of the viscoelastic surfactant fracturing fluid of the invention. 0.3 of CELQUAT® H-100 was added to 90 ml of water, as an aqueous solvent, under continuous agitation for 30 minutes, and then 0.1 ml of Product 239, a clay stabilizer from Specialty Product, was added, followed by 2.4 ml of ethylene glycol monobutyl ether and then 7.6 ml of lecithin while under agitation. The pH of the solution was adjusted to 10.0 using a 30% NaOH solution and agitation was continued for another 10 minutes. The fluid was placed on the Fann 50C viscometer and sheared at 100 s⁻¹ constantly while the temperature was raised to the test temperature. FIG. 11 illustrates the Theological measurements of the fluid and demonstrates that the inventive fluid of the invention is compatible with additional typical clay stabilizers used by the industry

Example 9

A sample of VES fluid was prepared by adding 0.3 g of CELQUAT® H-100 quaternary amine to 90 ml of water under continuous agitation for 30 minutes, followed by 2.4 ml of EGMBE (ethylene glycol monobutyl ether) and then 7.6 ml of lecithin while under agitation. The pH of the solution was adjusted to approximately 10.0 using a 30% NaOH solution and the solution was agitated for another 10 minutes. A breaker package (0.6 ml of triethylcitrate and 0.06 g of ammonium persulfate) was added into the fluid immediately prior to pumping the fluid into a permeameter as described in the paragraph below.

Core flow test was done on a homemade permeameter. A 2″ long and 1″ diameter Berea sandstone core was cut and degassed and then placed in a 3% KCl solution for at least 24 hrs under vacuum. The initial permeability of the core was obtained with 3% KCl at 180 F by pumping 3% KCl at constant flow rate from production direction. After the initial perm was obtained, the VES fluid from the above paragraph (with breaker) was pumped through the core from injection direction (reverse direction) and at least 30-minute fluid leak-off was collected. The core was then shut-in for at least 12 hrs at 180 F. A 3% KCl solution was then pumped through the core from the production direction at constant flow rate to regain the perm of the core. The regained permeability of the core was 98% of the original permeability of the core.

From the foregoing, it will be observed that numerous variations and modifications may be effected without departing from the true spirit and scope of the novel concepts of the invention. 

1. A method of fracturing a hydrocarbon-bearing formation which comprises introducing to the formation a viscoelastic vesicular fracturing fluid comprising (a) at least one surfactant; (b) at least one quaternary amine polyelectrolyte; (c) water; and (d) a non-aqueous solvent.
 2. The method of claim 1, wherein the polyelectrolyte is a quaternary amine of a cellulose ether, aminoalkyl cellulose, aminocarbamoyl cellulose, hydroxyalkylcellulose or betainized cellulose aminoamides.
 3. The method of claim 1, wherein the polyelectrolyte is a cellulose ether represented by the overall structural formula:

wherein: R_(cell) is the residue of an anhydroglucose repeat unit; t is 0 or 1; X is oxygen; z is from 50 to about 20,000; and each R₁, R₂ and R₃ is individually represented by the substituent structural formula:

wherein: A⁻ is an anion; a is an integer of from 1 to about 3; m is an integer of from 0 to about 6; n is an integer greater than or equal to 0, provided that the level of cationic substitution, CS, defined by the average moles of quaternary nitrogen atoms per mole anhydroglucose repeat unit is greater than 0; p is an integer of from 0 to about 6; q is 0 or 1; each R₅ and R₇ is individually ethylene, a propylene or a hydroxypropylene; R₆ is a di- or trivalent, cyclic, branched or straight chain, saturated or unsaturated hydrocarbon having from 2 to about 6 carbon atoms, provided there are at least 2 carbon atoms between the nitrogen atom and any oxygen atom; R₈ is hydrogen, hydroxyl, R_(h), alkyl, carboxyl or alkali metal or amine carboxylate, or other terminal group provided that when q is 0 then R₈ is hydrogen or alkyl; each R₉, R₁₀ and R₁₁ is individually R_(h), alkyl, aryl, aralkyl, alkaryl, cycloalkyl, alkoxyaryl or alkoxyalkyl, having at least two carbon atoms separating the oxygen atom in the alkoxyaryl or alkoxyalkyl group from the nitrogen atom or together with R₆ forms a heterocyclic ring; R_(h) is a hydrophobic group containing an alkyl group having at least 8 carbon atoms; v is equal to the valence of A; y is 0 or 1, provided that when y is 0 then p and q are 0 and R₈ is hydrogen or other terminal group.
 4. The method of claim 3, wherein the cellulose ether is polyquaternium-4.
 5. The method of claim 1, wherein the water is fresh water or seawater.
 6. The method of claim 1, wherein the pH of the viscoelastic fluid is between from about 9.0 to about 11.0.
 7. The method of claim 1, wherein the at least one surfactant is an anionic surfactant or a mixture of a cationic and an ionic surfactant.
 8. (canceled.)
 9. (canceled.)
 10. (canceled.)
 11. (canceled.)
 12. The method of claim 1, wherein the fluid further comprises an internal breaker.
 13. The method of claim 12, wherein the internal breaker comprises at least one oxidative breaker and/or at least one acid forming agent.
 14. The method of claim 13, wherein the oxidative breaker is at least one member selected from a persulfate, peroxidizer, sodium perborate, sodium bromate, sodium perforate, potassium iodate, potassium periodate, sodium chlorite, sodium hypochlorite, lithium hypochlorite or calcium hypochlorite.
 15. The method of claim 13, wherein the at least one acid forming agent is initially inert but slowly hydrolyzes in the fracturing fluid to produce a Bronsted acid, thereby gradually lowering the pH of the fluid to activate the oxidative breaker.
 16. The method of claim 15, wherein the acid forming agent is an organic anhydride, acyl halide, sulfonyl halide, benzylic halide or a low molecular weight ester.
 17. The method of claim 16, wherein the low molecular weight ester is ethyl acetate, 2-ethoxyethylacetate, ethylacetoacetate, triethylcitrate, methylbenzoate or dimethylphthalate.
 18. The method of claim 17, wherein the low molecular weight ester is trimethyl citrate.
 19. The method of claim 14, wherein the oxidative breaker is ammonium persulfate.
 20. The method of claim 18, wherein the oxidative breaker is ammonium persulfate.
 21. The method of claim 1, wherein the non-aqueous solvent comprises a linear, branched, or cyclic alcohol.
 22. A method of fracturing a subterranean formation comprising: (a) providing an aqueous-based hydraulic fracturing fluid comprising vesicles; and (b) pumping the fluid through a wellbore and into a formation at a pressure sufficient to fracture the formation; and further wherein the fracturing fluid comprises: (1) at least one surfactant; (2) at least one quaternary amine polyelectrolyte; (3) water; and (4) a non-aqueous solvent.
 23. The method of claim 22, wherein the polyelectrolyte is a derivative of carboxymethyl cellulose wherein at least one of the carboxymethyl groups are replaced by polyquaternary ammonium groups.
 24. The method of claim 22, wherein the vesicles have a diameter of between about 100 Å and about 50 microns.
 25. The method of claim 22, wherein the vesicles are unilamellar, multilamellar, or both.
 26. The method of claim 22, wherein the polyelectrolyte is a cellulose ether represented by the overall structural formula:

wherein: R_(cell) is the residue of an anhydroglucose repeat unit; t is 0 or 1; X is oxygen; z is from 50 to about 20,000; and each R₁, R₂ and R₃ is individually represented by the substituent structural formula:

wherein: A⁻ is an anion; a is an integer of from 1 to about 3; m is an integer of from 0 to about 6; n is an integer greater than or equal to 0, provided that the level of cationic substitution, CS, defined by the average moles of quaternary nitrogen atoms per mole anhydroglucose repeat unit is greater than 0; p is an integer of from 0 to about 6; q is 0 or 1; each R₅ and R₇ is individually ethylene, a propylene or a hydroxypropylene; R₆ is a di- or trivalent, cyclic, branched or straight chain, saturated or unsaturated hydrocarbon having from 2 to about 6 carbon atoms, provided there are at least 2 carbon atoms between the nitrogen atom and any oxygen atom; R₈ is hydrogen, hydroxyl, R_(h), alkyl, carboxyl or alkali metal or amine carboxylate, or other terminal group provided that when q is 0 then R₈ is hydrogen or alkyl; each R₉, R₁₀ and R₁₁ is individually R_(h), alkyl, aryl, aralkyl, alkaryl, cycloalkyl, alkoxyaryl or alkoxyalkyl, having at least two carbon atoms separating the oxygen atom in the alkoxyaryl or alkoxyalkyl group from the nitrogen atom or together with R₆ forms a heterocyclic ring; R_(h) is a hydrophobic group containing an alkyl group having at least 8 carbon atoms; v is equal to the valence of A; y is 0 or 1, provided that when y is 0 then p and q are 0 and R₈ is hydrogen or other terminal group.
 27. The method of claim 26, wherein the cellulose ether is polyquatemium-4. 